US20080032375A1 - Method and Fermenter for the Anaerobic Fermentation of Biological Waste - Google Patents

Method and Fermenter for the Anaerobic Fermentation of Biological Waste Download PDF

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US20080032375A1
US20080032375A1 US11/596,811 US59681105A US2008032375A1 US 20080032375 A1 US20080032375 A1 US 20080032375A1 US 59681105 A US59681105 A US 59681105A US 2008032375 A1 US2008032375 A1 US 2008032375A1
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reactor
fermenting
fermented product
fermenter
starting material
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Rudolf Hartmann
Hans Wuethrich
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
    • B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
    • B09B3/00—Destroying solid waste or transforming solid waste into something useful or harmless
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F27/00—Mixers with rotary stirring devices in fixed receptacles; Kneaders
    • B01F27/60—Mixers with rotary stirring devices in fixed receptacles; Kneaders with stirrers rotating about a horizontal or inclined axis
    • B01F27/70—Mixers with rotary stirring devices in fixed receptacles; Kneaders with stirrers rotating about a horizontal or inclined axis with paddles, blades or arms
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F35/00—Accessories for mixers; Auxiliary operations or auxiliary devices; Parts or details of general application
    • B01F35/71—Feed mechanisms
    • B01F35/712—Feed mechanisms for feeding fluids
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M21/00—Bioreactors or fermenters specially adapted for specific uses
    • C12M21/04—Bioreactors or fermenters specially adapted for specific uses for producing gas, e.g. biogas
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M27/00—Means for mixing, agitating or circulating fluids in the vessel
    • C12M27/02—Stirrer or mobile mixing elements
    • C12M27/06—Stirrer or mobile mixing elements with horizontal or inclined stirrer shaft or axis
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M41/00—Means for regulation, monitoring, measurement or control, e.g. flow regulation
    • C12M41/12—Means for regulation, monitoring, measurement or control, e.g. flow regulation of temperature
    • C12M41/18—Heat exchange systems, e.g. heat jackets or outer envelopes
    • C12M41/22—Heat exchange systems, e.g. heat jackets or outer envelopes in contact with the bioreactor walls
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M45/00—Means for pre-treatment of biological substances
    • C12M45/02—Means for pre-treatment of biological substances by mechanical forces; Stirring; Trituration; Comminuting
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M45/00—Means for pre-treatment of biological substances
    • C12M45/04—Phase separators; Separation of non fermentable material; Fractionation
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M45/00—Means for pre-treatment of biological substances
    • C12M45/20—Heating; Cooling
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F35/00—Accessories for mixers; Auxiliary operations or auxiliary devices; Parts or details of general application
    • B01F35/71—Feed mechanisms
    • B01F35/715—Feeding the components in several steps, e.g. successive steps
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F11/00—Treatment of sludge; Devices therefor
    • C02F11/02—Biological treatment
    • C02F11/04—Anaerobic treatment; Production of methane by such processes
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W10/00—Technologies for wastewater treatment
    • Y02W10/20—Sludge processing
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W30/00—Technologies for solid waste management
    • Y02W30/40—Bio-organic fraction processing; Production of fertilisers from the organic fraction of waste or refuse

Definitions

  • the invention relates to a method of anaerobic fermentation of biological waste in accordance with the preamble of claim 1 and a fermenter, especially for carrying out said method.
  • the percolation can be carried out, for example, in a box percolator according to WO 97/27158 A1. Also tests using a boiling percolator according to DE 101 42 906 A1 in which the percolation is carried out in the boiling range of the process water turned out to be promising.
  • the organically highly loaded exit water extracted from the percolator is supplied to a biogas plant for anaerobic decomposition, wherein the organic part is converted by means of methane bacteria and can be fed to biogas combustion via a gas-making pipeline for energy generation.
  • the afore-described aerobic treatment of the waste materials in a percolator has turned out to be extremely competitive with the anaerobic methods and has become increasingly important.
  • the impurity/high-gravity solids are conveyed and discharged to the center of the fermenting reactor via two conveying means.
  • the introduction and the extraction of starting material/fermented product is preferably carried out via a central conveying station by which the flow paths can be reversed to and from the inlet/outlet openings and thus appropriately varying material flow profiles can be formed in the fermenting reactor.
  • neighboring mixing blades of the agitator overlap in axial direction so that a complete mixing of the reactor content is ensured.
  • the agitator may have an especially simple design, when the agitating shaft thereof is supported on both sides in the reactor and the diameter is dimensioned such that the agitating shaft is sufficiently supported by the buoyancy occurring in the reactor.
  • the fermenting reactor is preferably horizontally arranged and has a circular or approximately trapezoidal cross-section. In the latter case two inclined surfaces and one horizontal surface disposed therebetween are formed in the area of the reactor bottom.
  • the gas injection nozzles for injecting biogas are disposed in the area of the two inclined surfaces in a reactor having a trapezoidal cross-section.
  • the gas injection nozzles can open in vertical direction, i.e. in parallel to the vertical reactor axis or normal to the inclined surfaces.
  • the shell of the fermenter can be heated.
  • a separate direct feeding of starting material can be provided through which starting material can be fed independently of the conveying station.
  • the assembly of the fermentation plant according to the invention is especially simple, when the fermenting reactor is composed of segments ready for transport which then are assembled on the spot at the construction site.
  • FIG. 1 shows a process diagram of the process according to the invention for anaerobic fermentation of biological waste comprising a fermenting reactor according to the invention
  • FIG. 2 shows a side view of the fermenting reactor of FIG. 1 ;
  • FIG. 3 shows a side view of another embodiment of a fermenting reactor
  • FIG. 4 is a cut top view of the fermenting reactor of FIG. 3 ;
  • FIG. 5 shows the fermenting reactor of FIG. 3 in segmental design
  • FIG. 6 shows the fermenting reactor of FIG. 2 in segmental design and comprising a high-gravity solids extracting system.
  • FIG. 1 the process diagram of a process according to the invention for anaerobic fermentation of biogenic waste is shown.
  • the introduced starting material 1 contains domestic waste (residual waste), for instance, having a comparatively high organic component, biological waste from the separate collection, organically highly loaded waste from food industry and excessively stored food, slaughtering waste, organically enriched slurry such as e.g. active slurry from sewage plants.
  • impurities 2 as well as impurity/high-gravity solids 4 occurring in process steps hereinafter described in detail are eliminated and the remaining starting material 1 is supplied to a fermenting reactor 16 .
  • fermenting gases are formed as metabolic product from the fermenting process, especially biogas 3 (methane gas) which is extracted to the top.
  • fermented product largely freed from the organic components is extracted after completion of the fermenting process and is supplied to further treatment, such as e.g. dehydration, drying or composting.
  • further treatment such as e.g. dehydration, drying or composting.
  • fermented product from residual waste must be deposited or burnt or at least recovered into substitute fuels.
  • Fermented product from biological waste or renewable raw materials can be used as fertilizer or soil conditioner after dehydration and further composting.
  • the entering starting material 1 is thus decomposed into impurity/high-gravity solids 2 , 4 , fermented product 5 and biogas 3 .
  • the starting material 1 fed is initially supplied to a mechanical accepting and preparation plant 8 in which the impurity solids 2 are sorted, crashed and extracted. Moreover, in this accepting and preparation plant 8 excessively stored food is unpacked and loading material and liquid waste, by which the dry matter content is adjusted, are added and conditioned.
  • the prepared and conditioned starting material is then fed to a pump collecting tank 9 and there possibly mixed with sewage 7 occurring during purification of high-gravity solids according to FIG. 6 , as will be described further below.
  • the collecting tank 9 is connected via a pipeline 12 and slides 11 to a central pump/conveying station 10 by which practically all substantial material flows of the plant are controlled.
  • the pump/conveying station 10 can be operated both in suction and in pressure operation so that either starting material 1 is conveyed from the collecting tank 9 via pipelines 14 and appropriately adjusted slides 11 to inlet openings 15 or fermented product 5 can be extracted via the pipelines 14 and appropriately reversed slides 11 as well as impurity/high-gravity solids can be extracted via a central extract opening 16 . 3 from the fermenting reactor 16 .
  • the fermenting reactor 16 has an approximately cylindrical structure and is horizontally disposed, wherein along its outer diameter and its length a plurality of inlet and outlet openings 15 and the central extract opening 16 . 3 are provided.
  • the inlet/outlet openings 15 can be used, depending on the control via the central pump/conveying station 10 and on the appropriate adjustment of the slides 11 , as inlet opening for starting material or outlet opening for fermented product. As indicated in broken lines in FIG. 2 , by this adequate control a desired material flow between the inlet/outlet openings 15 can be adjusted which is selected such that an optimum mixing of the fermented product is ensured.
  • the pump/conveying station 10 permits to extract fermented product via one of the inlet/outlet openings 15 , for instance, and then to re-feed it as inoculum via a different one of the inlet/outlet openings 15 .
  • the guiding of the flow for example, is chosen such that inside the reactor no substantial differences in concentration of organic acids and of ammonium are adjusted so that the fermenting process can take place in the predetermined manner.
  • rotary piston, displacement or suction/pressure tank systems are employed as conveying means, which are used, for instance, in agriculture or for sewerage clearance.
  • conveying means which are used, for instance, in agriculture or for sewerage clearance.
  • FIG. 2 Further functions will be illustrated hereinafter by way of FIG. 2 .
  • the cylindrical, horizontally disposed fermenting reactor 16 shown in FIGS. 1 and 2 comprises an agitator 22 driven by two torque-based gear motors 22 . 1 mounted on the face of the reactor 16 .
  • Said motors are controlled via frequency converters and thus their direction of rotation can be reversed periodically and/or in response to other operating parameters.
  • Agitating arms 22 . 2 evenly distributed along the circumference or disposed in a plane are fastened to an agitator shaft 22 . 4 and extend in radial direction outwardly toward the circumferential wall of the fermenting reactor.
  • Agitator blades 22 . 3 extending in parallel to the axis are fastened to the radially outer end portions of the agitator arms 22 . 2 , wherein the radial length of the agitator arms 22 . 2 is selected such that the agitator blades 22 . 3 skim over the fermenting sludge level 20 . 1 during rotation so that a forming scum layer is destroyed or at least mixed.
  • the axial length of the fermenting reactor 16 may easily be more than 30 meters.
  • an agitator shaft 22 . 4 is dimensioned so that it is supported by the buoyancy of the fermenting sludge 20 in the fermenting reactor 16 and thus cannot sag—hence an expensive mounting inside the reactor chamber can be dispensed with.
  • two settled material discharge means are provided which are in the form of two interacting pusher plates 23 in the embodiment shown in FIG. 1 . The latter convey the settled material in axial direction to the centrally disposed extract opening 16 . 3 through which the settled material (high-gravity/impurity solids) can be
  • the anaerobic fermenting reactor (fermenter) is provided with plural inlet openings and fermented product outlet openings by which starting material or fermented product (the latter as inoculum) can be supplied and/or fermented product can be extracted.
  • the metabolic process can be controlled so that the concentration of organic acids and ammonium inside the fermenting reactor can be most largely evened.
  • the conventional plug-flow solutions described in the beginning in the different longitudinal sections of the reactor different concentrations are brought about which considerably inhibit or even bring the fermenting process to a standstill and thus considerably extend the holding time.
  • the fermented product is partly mixed and inoculum is introduced along the flow path of the waste to be treated inside the reactor—this results in the fact that the holding time can be reduced to a fraction of the holding times required in prior art. It is expected that the holding time in the solution according to the invention is less than two days.
  • the fermented product is thoroughly mixed inside the fermenting reactor via a mechanical agitator and/or by biogas injection so that the fermenting process is further improved.
  • the direction of rotation of the agitator is reversed during the fermenting process so as to further improve thorough mixing.
  • the biogas is preferably injected into the fermenting reactor by gas injection nozzles disposed in the reactor bottom.
  • the gas injection nozzles are preferably combined in fields and are successively controlled.
  • the gas injection is controlled such that the scum is broken up in the area of the respectively controlled field. flow of the waste between the inlet opening and the outlet opening.
  • EP 0 476 217 A1 a heatable fermenter is disclosed in which starting material and sludge material are supplied to the fermenter as bacteria inoculum and the sludge material formed is transported to a sludge material outlet via an agitator.
  • inoculum may also be provided in the Valorga method according to EP 0 192 900 B1 described in the beginning.
  • a fermenting method for waste in fluid form i.e. having a dry matter content (German abbreviation: TS) of less than 25%
  • TS dry matter content
  • a multi-chamber reactor is used for this purpose, wherein the fermented product can be transported from an inlet opening through the chambers to an outlet opening via an agitator.
  • a common gas chamber from which the biogas formed during the fermenting process is extracted is allocated to the multi-chamber reactor.
  • the metabolism can be individually controlled in the individual chambers by a different conduct of the process, for instance via heat exchangers, addition of inoculum etc.
  • EP 0 794 247 A1 discloses a fermenter in which the fermented product is introduced to a rotating drum in which a spiral is arranged.
  • the fermented product is guided in plug shape from the inlet to the sludge material outlet via said spiral.
  • This supply can take place by forward and backward rotation of the drum, wherein the forward rotation, i.e. the transportation of the fermented product in the direction of the fermented product outlet takes longer than in the opposite direction so that a predetermined holding time of the fermented product is reached.
  • the object underlying the invention is to provide a method of anaerobic fermentation of biological waste as well as a fermenter by which the holding time can be substantially reduced vis-à-vis conventional solutions. discharged.
  • the two pusher plates 23 are driven by a cylinder/piston unit 23 . 1 adapted to be operated electrically or hydraulically.
  • the pusher plates 23 perform strokes in the directions of the arrows 23 . 2 so as to convey the settled material in the direction of the extract opening 16 . 3 .
  • the agitator blades 22 . 3 end somewhat above the pusher plates 23 so that the settled material is conveyed downward inside the reactor by the agitator 22 .
  • the gas chamber 3 . 1 is secured by a safety means 33 so that no excessive pressure can build up.
  • the above-mentioned control of the gear motors 22 . 1 of the agitator 22 is designed such that the settled material 4 is introduced evenly from both sides into a discharge shaft of the pusher plates 23 by reversing the direction of rotation and appropriate timing.
  • a shell 16 . 1 of the fermenting reactor 16 is provided with insulation 16 . 1 to maintain a predetermined fermenting temperature.
  • This fermenting temperature can be adjusted by means of heating pockets 18 ( FIG. 2 ) distributed along the outer circumference of the fermenting reactor 16 and can be controlled by the plant control in such way that inside the reactor the predetermined temperature profile is adjusted.
  • starting material can be further introduced via direct charging.
  • Said starting material is branched off by an appropriately adjusted slide 11 and heated to processing temperature by a heat exchanger 17 .
  • the heat exchanger 17 is surrounded by a heating shell 17 . 3 and includes a guiding tube 17 . 2 heated thereby in which a conveyor spiral 17 . 1 is disposed through which the starting material is introduced and further conveyed.
  • the starting material 1 heated to processing temperature is then conveyed into the interior of the reactor via a further slide 11 and a spiral conveyor 32 , for instance, wherein the spiral conveyor 32 enters below the fermenting sludge level 20 . 1 .
  • Preheated starting material can be branched off downstream of the heat exchanger 17 via a further slide 11 and can be guided to the central pump/conveying station 10 via a branch line 13 .
  • the extract opening 16 . 3 can be formed by three or more parallel extract areas 16 . 3 a, 16 . 3 b, 16 . 3 c through which the settled material conveyed by the pusher plates 23 can be extracted toward the conveying pipelines 14 by way of slides 11 a, 11 b, 11 c.
  • FIG. 2 it is also illustrated very clearly that the agitator blades 22 . 3 shovel the settled material to the pusher plates 23 and, depending on the control of the slides 11 , via the pump/conveying station 10 inside the fermenting reactor 16 different flow directions 20 . 2 of fermenting sludge are adjustable which result in an intense mixing and evening of the concentration inside the fermenting reactor 16 .
  • the afore-described cylindrical reactor shape can be manufactured in a comparatively simple manner and is superior to other solutions as regards the compressive strength. Under certain conditions it can also be necessary, however, to design the fermenting reactor 16 to have a different geometry. Such embodiment is illustrated in FIGS. 3 and 4 .
  • the fermenting reactor 16 has an approximately rectangular cross-section, the bottom being formed by two inclined surfaces 16 . 4 which are connected to each other by a horizontally extending horizontal surface 16 . 5 .
  • the two pusher plates 23 and the extract opening 16 . 3 a, b, c are formed.
  • the inlet and outlet openings 15 are then provided in the side walls of the fermenting reactor 16 extending in vertical direction.
  • the material flows are controlled—as in the afore-described embodiment—by the central pump/conveying station 10 so that inside the fermenting reactor 16 in turn different material flow paths 20 . 2 can be adjusted.
  • a gas injection plant is used instead of a mechanical agitator 22 , i.e. a pneumatic agitation is used.
  • the gas injection plant has a plurality of nozzles 30 . 1 which preferably open in the inclined surfaces 16 . 4 of the fermenting reactor 16 .
  • FIG. 3 two different nozzle orifice areas are shown.
  • the nozzles 30 . 1 extend approximately normal to the inclined surface 16 . 4
  • the nozzles 30 . 1 in the right-hand part are arranged in parallel to the normal axis (vertical in FIG. 3 ) of the fermenting reactor 16 .
  • the injected gas flows into the reactor chamber obliquely with respect to the normal axis, whereas in the embodiment shown on the right it is injected in parallel to the normal axis.
  • biogas For a pneumatic conveying and circulation of the fermenting sludge 20 biogas is used which is sucked from the gas dome 3 . 2 by means of a compressor 26 and then is guided via a gas injecting line 27 as well as via plural control valves 28 , 29 and connected branch lines to a respective nozzle field 30 consisting of a plurality of nozzles 30 . 1 .
  • the fields 30 are arranged successively along the inclined surfaces 16 . 4 in the longitudinal direction of the reactor (normal to the plane of projection in FIG. 3 ), wherein biogas can be separately applied to each field 30 by the system control.
  • the compressor 26 is arranged above the fermenting sludge level 20 . 1 by the measure H 4 so that in the case of standstill of the compressor 26 no fermenting sludge 20 can penetrate the compressor via the gas injecting line 27 .
  • the minimum gas pressure required for circulating the fermenting sludge 20 approximately corresponds to the barometric height (H2 ⁇ 1.5 (bar)) of the filling level required to overcome the pipeline resistance.
  • the number of gas injection nozzles 30 . 1 per nozzle field 30 also depends on the dimensions x, y, i.e. the length and the width of the nozzle fields 30 , wherein between 8 and 16 nozzles are disposed per square meter bottom area depending on the height H 2 .
  • the fields 30 are successively subjected to pressurized gas in longitudinal direction by alternately switching the control valves 28 , 29 .
  • the fermenting sludge 20 is displaced by the ascending gas bubble and is moved by the occurring suction in the direction of the arrow according to FIG. 3 , wherein the nozzles 30 . 1 opening in vertical direction initially bring about an upwardly directed flow, while the obliquely opening nozzles 30 . 1 deflect the fermenting sludge flow to the right.
  • the circulation can also take place inversely to the direction of the arrow by an appropriate control of the pump/conveying station 10 and the gas injection nozzles 30 . 1 .
  • the time of applying gas via the nozzles 30 . 1 depends on the height of the tank H 2 , H 3 and the adjusted dry matter content (TS). Gas is applied to each field 30 until a forming scum 31 . 1 is torn.
  • the fermenting reactor 16 according to the invention can have a considerable length (30 m). Therefore it is not possible to transport the finished reactor vessel to the construction site. So far it has had to be manufactured on the spot, i.e. at the construction site so that considerable manufacturing expenditure is required.
  • the length L 1 of the vessel is divided into elements ready for transport having a length of about 12 to 15 m and a width b 1 of about 3 to 4 m.
  • the building height H 1 approximately corresponds to a transport length of about 15 m and a width B 1 (corresponding to the width of the inclined surfaces 16 . 4 and the horizontal surface 16 . 5 in horizontal direction) of about 4 m.
  • the vessel is divided into a plurality of segments each having a width b 1 of 3 to 4 m and the aforementioned length of about 12 to 15 m so that a comparatively easy transport to the construction site and a quick assembly on the spot are possible.
  • FIG. 6 a high-gravity solids outlet means is shown.
  • the high-gravity solids settled by the effect of the mechanical agitator 22 or by the pneumatic conveying through the nozzles 30 . 1 and conveyed from the pusher plates 23 to the centrally arranged extract openings 16 . 3 first get into a discharging spiral conveyor 24 feeding an inclined conveyor 25 .
  • the high-gravity solids 4 are conveyed obliquely upwards to a cleansing plant 25 . 1 provided above the fermenting sludge level 20 . 1 . In said cleansing plant 25 .
  • the soiled high-gravity solids 4 are conveyed through a screening basket to which cleaning water 6 is applied from outside for rinsing out the soil so that cleaned high-gravity solids 4 . 1 are extracted.
  • the soiled cleaning water 7 is returned to the collecting tank 9 (see FIGS. 1 and 2 ) and is used for adjusting the dry matter (TS) content there.
  • the cleaned high-gravity solids 4 . 1 can be deposited or supplied to any other utilization. Industrial water or fresh water, for instance, can be used as cleaning water 6 .
  • the fermented product 5 occurring in the foregoing processes is subjected to further treatment, for example dehydration, drying or composting.
  • the agitating movement (mechanical/pneumatic) is assisted by the afore-described guiding of the flow of the fermenting sludge inside the fermenting reactor 16 along the flow lines 20 . 2 in FIGS. 2 and 3 , but primarily the inoculation of the introduced starting material with active bacteria mass (inoculum) from the outlet or in different positions at the reactor 16 is improved and thus the biological reaction is accelerated.
  • gas inlet nozzles can be added to the gas inlet nozzles according to FIG. 3 .
  • the gas injection nozzles can be used also in a fermenting reactor having a circular cross-section in accordance with FIG. 1 .
  • a method for anaerobic fermentation of biological waste and a fermenter for carrying out said method are disclosed.
  • the starting material in other words, the biological waste for treatment, is introduced through several inlet openings distributed along the reactor height and/or length and/or fermented product is extracted through several fermented product outlet openings.

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  • Chemical Kinetics & Catalysis (AREA)
  • Analytical Chemistry (AREA)
  • Thermal Sciences (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Physics & Mathematics (AREA)
  • Environmental & Geological Engineering (AREA)
  • Mechanical Engineering (AREA)
  • Processing Of Solid Wastes (AREA)
  • Treatment Of Sludge (AREA)
  • Fertilizers (AREA)
  • Apparatus Associated With Microorganisms And Enzymes (AREA)
  • Preparation Of Compounds By Using Micro-Organisms (AREA)
  • Mixers With Rotating Receptacles And Mixers With Vibration Mechanisms (AREA)
US11/596,811 2004-05-19 2005-05-19 Method and Fermenter for the Anaerobic Fermentation of Biological Waste Abandoned US20080032375A1 (en)

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DE102004025318.8 2004-05-19
DE200410025318 DE102004025318A1 (de) 2004-05-19 2004-05-19 Verfahren und Vergärungsanlage zum anaeroben Vergären von biogenem Abfall
PCT/EP2005/005452 WO2005113469A1 (de) 2004-05-19 2005-05-19 Verfahren und vergärungsanlage zum anaeroben vergären von biogenem abfall

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BR (1) BRPI0510144A (ja)
CA (1) CA2567146A1 (ja)
DE (1) DE102004025318A1 (ja)
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Cited By (13)

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US20080138888A1 (en) * 2005-01-26 2008-06-12 Walter Schmid Fermenter Comprising An Agitator
US20110236965A1 (en) * 2008-02-01 2011-09-29 Rick Claypool Panelized drum system
US20120135492A1 (en) * 2010-04-14 2012-05-31 Straeter James E Apparatus and method of using an agricultural waste digester and biogas generation system
EP2562243A1 (en) * 2011-08-26 2013-02-27 Thöni Industriebetriebe GmbH Operation of fermentation devices
CN103374521A (zh) * 2013-02-04 2013-10-30 中国科学院青岛生物能源与过程研究所 一种机械与水力组合搅拌的秸秆厌氧发酵制沼气工程装置
US20130295625A1 (en) * 2010-11-30 2013-11-07 Hyundai Engineering & Construction Co., Ltd. Apparatus and Method for Treating Organic Waste
US9157100B2 (en) 2012-06-15 2015-10-13 Coskata, Inc. Integrated processes for bioconverting syngas to oxygenated organic compound with sulfur supply
CN105462821A (zh) * 2016-01-15 2016-04-06 河南省立丰实业有限公司 大型卧式隧道窑型螺旋连续干式厌氧发酵设备
CN107904143A (zh) * 2017-11-17 2018-04-13 湖州润迪环保科技有限公司 一种可控卸料速度的生物酶搅拌装置
US20190062682A1 (en) * 2017-08-29 2019-02-28 Hitachi Zosen Inova Ag Process for optimizing the operation of a plug-flow fermenter for the anaerobic fermentation of organic wastes
WO2019166620A1 (en) * 2018-03-01 2019-09-06 Doranova Oy Anaerobic digestion reactor and plant
CN110437986A (zh) * 2019-07-25 2019-11-12 杭州能源环境工程有限公司 一种厌氧发酵耦合沼渣静态发酵高效产沼的系统及工艺
CN117343827A (zh) * 2023-12-05 2024-01-05 格莱德(福建)生物科技有限公司 一种方便加料的犬饲料厌氧发酵装置

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JP2007229638A (ja) * 2006-03-01 2007-09-13 Sumitomo Heavy Ind Ltd 廃棄物処理装置
DE102007024378B4 (de) 2007-05-23 2009-06-04 Beck, Jürgen, Dr. Fermenter zur Erzeugung von Biogas aus pumpbarem organischen Material
CN101812400A (zh) * 2009-12-22 2010-08-25 上海济兴能源环保技术有限公司 立式干法厌氧发酵装置
JP5759674B2 (ja) * 2010-01-14 2015-08-05 株式会社タクマ 横置き型撹拌システム用撹拌軸
CN102321524B (zh) * 2011-06-13 2013-07-17 廖英俊 再生燃料生产机及生产燃气的方法
EP2669364B1 (en) * 2012-05-28 2017-07-19 Energiutvecklarna Norden AB Biogas reactor
JP2014176784A (ja) * 2013-03-13 2014-09-25 Zukosha:Kk メタン発酵システム
NO20130626A1 (no) 2013-05-03 2014-11-04 Sewage Treat Plants As Behandlingsanordning for organisk materiale
JP6410277B1 (ja) * 2017-11-08 2018-10-24 株式会社タクマ メタン発酵システム及びメタン発酵方法
DE102019201445A1 (de) * 2019-02-05 2020-08-06 Kniele Gmbh Schräglagenmischer
BE1029384B9 (nl) * 2021-05-07 2023-01-16 Dranco Inrichting en werkwijze voor het verwerken van organisch materiaal

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US5269634A (en) * 1992-08-31 1993-12-14 University Of Florida Apparatus and method for sequential batch anaerobic composting of high-solids organic feedstocks

Cited By (17)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20080138888A1 (en) * 2005-01-26 2008-06-12 Walter Schmid Fermenter Comprising An Agitator
US7659108B2 (en) * 2005-01-26 2010-02-09 Kompogas Ag Fermenter comprising an agitator
US20110236965A1 (en) * 2008-02-01 2011-09-29 Rick Claypool Panelized drum system
US8871501B2 (en) * 2008-02-01 2014-10-28 Rick Claypool Panelized drum system
US20120135492A1 (en) * 2010-04-14 2012-05-31 Straeter James E Apparatus and method of using an agricultural waste digester and biogas generation system
US9382509B2 (en) * 2010-04-14 2016-07-05 James E. Straeter Apparatus and method of using an agricultural waste digester and biogas generation system
US20130295625A1 (en) * 2010-11-30 2013-11-07 Hyundai Engineering & Construction Co., Ltd. Apparatus and Method for Treating Organic Waste
EP2562243A1 (en) * 2011-08-26 2013-02-27 Thöni Industriebetriebe GmbH Operation of fermentation devices
US9157100B2 (en) 2012-06-15 2015-10-13 Coskata, Inc. Integrated processes for bioconverting syngas to oxygenated organic compound with sulfur supply
CN103374521A (zh) * 2013-02-04 2013-10-30 中国科学院青岛生物能源与过程研究所 一种机械与水力组合搅拌的秸秆厌氧发酵制沼气工程装置
CN105462821A (zh) * 2016-01-15 2016-04-06 河南省立丰实业有限公司 大型卧式隧道窑型螺旋连续干式厌氧发酵设备
US20190062682A1 (en) * 2017-08-29 2019-02-28 Hitachi Zosen Inova Ag Process for optimizing the operation of a plug-flow fermenter for the anaerobic fermentation of organic wastes
US10519408B2 (en) * 2017-08-29 2019-12-31 Hitachi Zosen Inova Ag Process for optimizing the operation of a plug-flow fermenter for the anaerobic fermentation of organic wastes
CN107904143A (zh) * 2017-11-17 2018-04-13 湖州润迪环保科技有限公司 一种可控卸料速度的生物酶搅拌装置
WO2019166620A1 (en) * 2018-03-01 2019-09-06 Doranova Oy Anaerobic digestion reactor and plant
CN110437986A (zh) * 2019-07-25 2019-11-12 杭州能源环境工程有限公司 一种厌氧发酵耦合沼渣静态发酵高效产沼的系统及工艺
CN117343827A (zh) * 2023-12-05 2024-01-05 格莱德(福建)生物科技有限公司 一种方便加料的犬饲料厌氧发酵装置

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CA2567146A1 (en) 2005-12-01
BRPI0510144A (pt) 2007-10-02
SG138615A1 (en) 2008-01-28
AU2005245120A1 (en) 2005-12-01
JP2007537850A (ja) 2007-12-27
KR20070011616A (ko) 2007-01-24
IL179393A0 (en) 2007-03-08
MXPA06013439A (es) 2007-06-22
ZA200609566B (en) 2007-12-27
RU2006141345A (ru) 2008-06-27
DE102004025318A1 (de) 2005-12-08
CN1989085A (zh) 2007-06-27
WO2005113469A1 (de) 2005-12-01
NO20065839L (no) 2006-12-15
HRP20060398A2 (en) 2007-03-31

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